Treating process



J. w. PAYNE TREATING PROCESS June 20, 1944.

HOPPER INVENTOR ZZa 6 E 0 NE 6 .1

J. W. PAYNE June 20, 1944.

- TREATING PROCESS Filed Dc. 28, 1940 5 Sheets-SheeC 2 E, m4 E NP a? WW m N T |N%A H 0 J June 20, 1944. AYNE 2,351,875

TREATING PROCESS 5 Sheets-Sheet I INVENTOR JflH/V WP/IV/Vf Filed Dec.

BY ATTORNEY June 20, 1944. J,W PA NE 2,351,875

TREAT ING PROCES 5 Filed Dec. 28, 1940 5 sheets-sheet 4 MM! I j INVENTOR .f0/-//V W PA Y/VE I ATTORN Y' TREATING PROCESS Filed Dec. 28, 1940 v5 Sheets-Sheet 5 Z, oomv /4 now/v BOTTOM 800 900 1,000 moo 1,200

ff/L/V raw/ 5m was, 056. F

OEG/it-E E 400 500 600 700 800 900 1,000 moo L200 1.300 L400 400 500 600 700 800900 000 moo 1.200 500 L400 DEGREE F. lNVENTOR JOHN 144 34mm. BY

ATTORNEY V. Patented June 20, 1944 TREATING PROCESS John W. Payne, Woodbnry, N. J., assignor to Socony-Vacuum Oil Company, Incorporated, New York, N. Y., a corporation of New York Application December 28, 1940, Serial No. 372,045

Claims.

This invention relates to the treatment of finely divided solid materials in the presence of gases or vapors. The invention is concerned particularly with processes of regenerating spent adsorbent type materials such as clays, activated clays, synthetic alumina-silica compositions, bauxite and the like which have been used in processes tending to exhaust the utility of the adsorbent by clogging, coating or impregnating it with liquid or solid material of a combustible nature, as, for example, oily, tarry, or carbonaceous materials in general, and which is regenerated for reuse by the application of heat to the spent adsorbent resulting in the driving off or burning off of inactive impurities. This application is a continuation-in-part of my copending application S. N. 321,164, filed February 28, 1940, now U. S. Patent No. 2,227,416, which, in turn, is a continuation-in-part of my application S. N. 210,150, filed May 26, 1938.

In regeneration of petroleum filter clays, for instance, as carried out today, the clay suffers a loss in efiiciency with each burning or regeneration until finally it cannot be regenerated to a sufiiciently high activity to warrant further regeneration, at which time the clay is discarded to waste. Since clays which have had a different number of burnings have different efficiencies, they are usually kept separate and separately classified. In general filter clays are only regenerated about five to eight times and practically never more than ten to fifteen times before they are thrown away.

The problem of regenerating clays is complicated by the sensitivity of the clays to high temperatures. While temperatures around 900 to 1150 F. are desired to burn off impurities from the clay, temperaturesaround 1300 F. may permanently injure the clay. Moreover, if the temperature falls too low, inefficient regeneration results. The problem of keeping the temperature of the clay within safe limits is'greatly increased since the combustion reaction involved in burning ofi the impurities evolves considerable amounts of heat and can very easily become so rapid as to get beyond control temporarily, either generally or locally. Probably one of the principal reasonsfor the successive losses in activity of regenerated clay is the fact a certain amount is overheated or underheated each treatment. In view of the fact most clays to be regenerated have more than enough carbonaceous material deposited thereon to furnish the heat required for regenerating, it is quite probable that present methods in general permit overheating; this appears to be true, moreover, from the fact it wouldbe extremely difiicult to control precisely the temperature of all the clay in present methods.

In the past various methods have been devised for carrying out the regeneration of spent filter clay. One of the first employed merely an open hearth upon which the clay was spread and burned. Today there are three principal types of burners in general use. In the first type the clay falls or cascades over baiiles set at about a 45 angle through a flue countercurrent to gases of combustion. In the second type the clay is regenerated in a rotary kiln slightly inclined from the horizontal. probably is the most commonly used, multiple hearth burners are employed. These multiple hearth furnaces or burners are substantially the same as used in the roasting of ore and are of either the Nichols-Herreshofi or Wedge type. In these burners the clay is slowly rabbled across each hearth, dropping from one to another until the bottom hearth is reached. In all of these commonly used burners the temperature is controlled principally by adding steam or water, cutting thefires, regulating clay feed rate and regulating the concentration of oxygen passed ,into the burner and therefore the rate of oxi dation.

The kilns or burners which are now in common use are relatively inefficient because of absence of proper temperature control for preventing overburning of clays, comparatively small throughout per unit volume of burner, and ineflicient utilization of the heat developed in buming the oil or other carbonaceous matter left on the clay, thus requiring considerable quantities of additional fuel to complete combustion.

Other apparatuses and methods have been proposed but have not displaced the three abovedescribed burners to any appreciable extent. This very fact that other burners have not been taken up by the art is believed conclusive that each one suggested is subject to limitations which prevent regenerations as efilcient as, orat least any more efficient than, those already enjoyed by the art.. While such a fact is not usually so conclusive, it is believed to be in the present case in view of the tremendous amounts of clay used and thrown away each year and the increased amount that is necessary because of the successive loss in efllciency. Moreover, in view of the fact that clays and like materials are not used in Just one industry but in many, with a universal desire existing for improvement, it is believed impossible that any method which effects any substantial improvement over those,

now employed could go unnoticed and undeveloped. This view may well be appreciated when it is realized that a single lube oil refinery in the petroleum industry alone may regenerate over 75,000 tons of filter clay each year.

As a result of my research I have striven to devise a method which would be commercially feasible for handling large quantities of clay and In the third type, which would permit burning off of inactive impurities from the clay at optimum temperatures whileat the same time affording such constant uniform heat control of all the clay under such closely controllable temperature conditions that substantially none of the clay would be subjected to a deleterious temperature. It is believed the improvedresults I obtain with my present method arelargely due'to the fact that this method permits burning of. clay under substantially these conditions. For the same reasons, my present process may be used with advantage in processes in general wherein finely divided solids are treated at closely controlled elevated temperatures. And, s nce my process does provide such efficient handling of large quantities of solid particle material, including the efficient contacting of same with gases or vapors, my invention is applicable to and includes processes in general for contacting any solid particle material with a gaseous agent whether any particular temperature control is necessary or desired or not.

It is an object of my invention to provide an eflicient process for contacting a flowing stream of sold particles with a countercurrently flowing gaseous agent.

Another object is to provide a method for the elevated heat treatmentof a moving stream of finely divided solids which permits uniform temperature control over each solid being treated throughout the period of its treatment.

Another object is to provide a. method of conducting a treatment wherein a moving stream of solid particles is directly contacted with gases or vapors which method afiords a uniform temperature control over each solid particle throughout its presence in the treatment and makes proper provision for passage of the gases or vapors through the solid particles.

A more spec fic object of the invention is to provide a method for subjecting a stream of porous adsorptive material of relatively small particle size, or other small particle size solids, to a heat treatment wherein the adsorptive material fiows countercurrent to gaseous medium in substantially a solid column of particles with proper gas paths formed therethrough and a uniform temperature control is maintained over each particle throughout its period of treatment.

Still another specific object of the invention is to provide a practical method for regenerating a mov ng stream of spent adsorptive material such 7 as filter clays and the like having carbonaceous impurities deposited thereon by reacting said carbonaceous impurities with a gaseous oxidizing medium which method suitablyflowsthe adsorptive material countercurrent to the gaseous medium and controls the temperature of the adsorptive material such that eflicient regeneration will be effected without subjecting the material to deleterious temperatures.

An important object is the continued regeneration of filter clays to a higher effloiency than heretofore obtained which substantially eliminates progressive degradation in efiiciency with successive regenerations.

Another object is the provision of a method capable of accomplishing high unit throughput per unit of capital invested and space occupied.

An important object is the provision of a method capable of being carried out in an apparatus having few moving parts and capable of easy and economical maintenance and operat on.

A further object is the provision of a method which permits more eflicient utilization of the heat developed in the apparatus.

These and other objects will appear from the following description of my invention.

In my present invention, treatments comprising the contacting of solid particles and gaseous agents are conducted preferably by flowing the particles through a treating zone countercurrently to the gaseous agent. Furthermore all of the solids are flowed substantially the same distance through the treating zone so that the treatment will be substantially uniform, and, in order to properly contact the solids and the gaseous agent in the treating zone, suitable provision is made for passage of the gaseous agent through the zone without causing channeling and undue disturbance of the general direction of flow of the solids. Still further, if it is desirable or necessary to maintain a close temperature control over the treatment, as, for example, in the regeneration of spent petroleum percolation clays by burning, I provide suitable temperature regulating means. The preferred methodof controlling temperature in the treating zone is by maintaining every solid partlcle'throughout its entire presence in the treating zone within sufficiently close indirect heat exchange with a suflicient amount of a properly temperature-controlled, circulating fluid heat exchange medium that the temperature of each and every solid particle while in the treating zone is kept within a proper treatingJtemperature range without any deleterious temperature occurring. This preferred procedure involving the use of temperature control is claimed in our copending application S. N. 321,164. There are also other methods of controlling temperature, it temperature control is desired. Thus the temperature may be controlled in a clay burning treatment, for instance, by recycling the flue gases so as to mix sufilcient flue gas with the incoming air that its effect as a diluent maintains the temperature between the minimum combustion temperature and the maximum combustion temperature that does notcausesubstantial heat damage to the clay. This latter type temperature control, however, will not permit the high clay throughput rate that is feasible by using the above-mentioned liquid heat exchange medium control. The important criterion to be observed in any temperature control method for burning combustible material 011 clay-type particles is to maintain the temperature of all the particles at all times during the burning between the minimum combustion temperature and the maximum combustion temperature that does not cause substantial damage to the particles. Again, there maybe occasions where temperature control is desired but it is not so difiicult to accomplish, or it does not require such exactness, as that for clay burning processes. In these instances it is apparent that various known types of temperature control may be employed.

Thus; as has been indicated above, the present invention may be used in the treatment of finely divided solids in general in order to change their physical or chemical character or both. Particularly typical of materials that may be treated by my invention are those spent filter clays or other adsorbents derived from the filtration of mineral oil products such as waxes, turbine and transformer oils and particularly the usual lubricating oils; or from filtration of vegetable oils; sugar liquors; etc., which spent clays or other adsorbents contain adsorbed combustible materials such as tarry, oily or carbonaceous matters and are regenerated for re-use by the heating or burning of the combustible material adsorbed thereon. In some instances it may be desirable to burn off only inactive carbonaceous impurities while carbonizing a part of the carbonaceous impurities to form an active carbon layer on the adsorbent.

Other typical materials which may be treated are catalytic materials composed of solid particles which have been used in some catalytic process of refining or conversion until sufficiently contaminated with impurities that regeneration or revivification is required or desirable and wherein the inactive impurities deposited on the catalyst are removed by treating the catalytic material at elevated temperatures. For instance, in the catalytic cracking of petroleum oils using a finely divided solid catalyst material, e. g., clay-type catalysts, the catalyst becomes contaminated with a carbonaceous deposit of the nature of coke which must be removed from time to time in order to regenerate the catalyst, and this removal is usually effected by burning oil the impurities at closely controlled elevated temperatures. Such catalyst treatments involve special problems and form the subject matter of the co-pending application S. N. 321,184 filed February 28, 1940.

For convenience the present process will be described in detail with respect to regeneration of filter clay. However, it is to be understood the invention is not limited thereto but is directed to the whole field of regeneration of spent adsorbents by burning off inactive impurities as well as to the initial preparation of same, when necessary, including activating, drying, hardening and the like by the application of heat. Likewise the present process, as has been stated, may be used to advantage for the treatment of solid particles in general, as, for instance, in roasting of ores. 'drying processes, adsorption and absorption processes, etc., and it is obvious that in some of these treatments no temperature control of any kind is required. Moreover, for some treatments it may be desired to contact a stationary, rather than moving, column or bed of finely divided particles. Since the present invention afiords such eflicient means of contacting the solids with gases, whether the solids are moving through the chamber or are being held in place therein, it is to be understood that treatments of stationary masses also are within the purview of this invention, although treatment of moving masses is preferred and will be described hereinafter.

In order that the invention may be readily understood, reference is now made to the accompanying drawings showing preferred embodiments of means for carrying out my present prrocess and wherein:

Fig. 1 is a general schematic drawing of one embodiment of an apparatus suitable for carrying out my invention;

Fig. 2 is a vertical section of a portion thereof;

Fig. 3 is a cross-section on the line 3-3 of Fig. 2;

Fig. 4 is a perspective view of typical interior arrangements within the apparatus;

Fig. 5 is a part elevation in section of an alternate form of apparatus suitable for carrying out my invention which omits the heat exchanger zones shown in Fig. 1;

Fig. 6 is a cross-section on the line 6--6 of Fig. 5;

Fig. '7 is a perspective view of a preferred head-- er structure for the heat transfer tubes of the alternate form shown in Fig. 5. g

Fig. 8 is a cross-section taken on the line 8--8 of Fig. 5; I

Fig. 9 is a cross-section taken -on the line 9- of Fig. 5;

Fig. 10 is a perspective view of a portion of another alternate form of an apparatus suitable for carrying out my invention showing an optional form of bailie structure, the view being taken at an angle somewhat below the horizontal looking up underneath the bailles;

Fig. 11 is a horizontal cross-sectional view of an apparatus containing internal structure of the type shown in Fig. 10;

Fig. 12 is a graph showing temperature control with variation of combustible materials on the solids; and r I Fig. 13 is a graph showing temperature control over a prolonged operation-using substantially the same feed.

Referring to Fig. 1, l0 indicates a burner or kiln in which there is housed a burning zone II, a preheating zone l2, and an after-cooler I3. Spent adsorbent or other solids to be treated, stored in'hopper I4 is fed to the upper end of the regeneration apparatus through a throat l6, and thereafter the adsorbent passes downward through zones I2, I I, and I3, and is removed from the apparatus in revivified or treated condition by some device It, which may preferably be a star wheel mechanism or some similar device for enabling the removal of adsorbent irrespective of the pressure maintained within the casing l0.

Air, or other suitable gaseous agent, under pressure is fed through inlet 11, and passes upward through the casing III in countercurrent relationship to the descending adsorbent, passing successively through zones II, II, and I2. The air departs from the apparatus through outlet l8 and is led into separator l9, which is a dust separator, preferably of the usual well-known cyclone type wherein fines and dust, if any, are separated from the moving stream of air. These separated materials are removed from or returned to the system through pipe 20-and air or flue gas is finally discharged through pipe 2|. It is obvious that these arrangements permit the operation within the case to be carried out at pressures below, near, or materially in excess of atmospheric pressure.

Within the case III, the functions carried out within the three zones are as follows: In zone It incoming air is preheated by contact with burned adsorbent, the adsorbent at the same time being cooled. In zone H a combustion occurs in which the carbonaceous impurities are burned from the adsorbent. In zone l2 another heat exchange occurs in which the hot flue gases are cooled and preheat the incoming adsorbent.

The rate and path of flow of air and adsorbent is so adjusted with respect to each other that the supporting effect of the rising column of air does not interfere with the uniform downward flow of the column of adsorbent. Optimum conditions are reached when the velocity of air' isquite high and in most cases it appears to be preferable that the velocity of the air is just short of that which will prevent uniform progress'of the adsorbent through the apparatus. In the event a combustible material such as bonechar is being regenerated, an inert gas, if any, will wholly or largely replace air andregeneration effected by heat alone, the inert gas "sweeping out the vaporized impurities being preferably introduced into the apparatus in the manner disclosed for the air. In case other gases are used in place of or in addition to air, they may be introduced through air inlet I! or separate inlets may be provided.

In the regeneration of spent petroleum filter clays, for instance, as stated above', it may not always be desired to burn 013 all the petroleum carbonaceous impurities but rather only inactive impurities. This may be done by reducing the amount of air or concentration of oxygen to a sufiicient extent to only burn oiI a part of the petroleum impurities, the remainder being carbonized to form an active carbon layer on the clay. The concentration of oxygen may be reduced by merely reducing the amount of air or by replacing a part or all of it with steam or inert gases. For some oils, notably solvent refined petroleum oils, yieldsfrom such carbonized clays are from-two to four times as great as from the same clay regenerated by complete burning. The use of carbonized clays for filtering solvent refined oils forms the subject matter of a co-pending case Serial Number 275,673, now Patent 2,245,016, filed May 25, 1939, and the carbonizing of petroleum filter clays by processes in general rather than only the particular one herein disclosed forms the subject matter of the copending application Serial Number 275,672, filed May 25,1939.

When combustion occurs under the circumstances above outlined in the presence of spent thetreating zone in one direction and the air in the other direction without either being al lowed to channel or fiow in a stream by itself without suflicient contact with the other medium. Furthermore, since my process is particularly directed to treatments of relatively small particles, such as percolation clays, ores to be roasted, etc., which small particles pack together sufiiciently that practically no gas voids are left between them, I have found that in order to successfully treat these small particles by my present process I must provide for suitable passage of the gas through the particles. In order to provide feasible passage, I baflie the gas and particles to form continuous, substantially particle-free passages for the gas which permits the gas therein to directly contact particles along I at least one edge of the passages, or I at least redistribute the particles and gaseous agent at adsorbentcontaining carbonaceous impurities and air under pressure and in the 8.0861106 of other agencies, there is a decided tendency to burning in'a concentrated zone at extremely high temperatures, ruinous to most adsorbents. Likewise in operations in general of this type wherein there is a considerable consumption, evolution or application of heat there is a tendency for localized or even general overe or underheating. In order to control this tendency and suppress it, the burning zone is equipped with heat transfer tubes 22, through which there is circulated a fluid heat transfer-medium which enters by pipe 23, leaves by pipe 24, and is circulated under the impulses produced by pump 25. Headers 32 connect pipes 23 and 24 of the external circuit with tubes 22 and areof any suitable construction which permits the clay to gravitate on through the space between the tubes.

In order that control of the temperature of this example, as making up losses or shutting down the system, there is provided a pipe connection 28. Tubes 22a in the heat exchanger zones 12 and I3 serve merely as spacing tubes for baffies 29.

A most important feature of the invention and one upon which the successful carrying out of the operation is largely dependent, is the provision of a proper treating or burning zone. To properly carry out the steps of the operation disclosed herein using countercurrent flow, the adsorbent must pass at a practical rate through sufiiciently frequent intervals that there is no such extended portion of downfiowing particles up through which gaseous agent must flow as to cause difiiculties, such as "boiling of the clay, in these portions.

Therefore, I have found that the structure of the treating or burning zones for carrying out a preferred operation where close temperature control is desired have two principal requirements, namely, suitable passage means, for circulating fluid heat exchange medium and suitable baflle means for the solids and gaseous agent. The passage means should be so arranged as to keep temperature-controlled, circulating fluid heat exchange medium within sufilciently close proximity to each and every solid particle in the zone throughout their entire presence in the zone that proper temperature control of each particle may be had. The particular arrangement or provision of the fiuid heat exchange medium throughout the zone is especially important and will be discussed more in detail hereinafter. The baffle means should be such as to (1) cause all the solids to have about the same length of fiow through the zone, (2) redistribute the gaseous agent and solids so as to prevent channeling, (3) aid in heat transfer, (4) provide adequate passage way for the gaseous agent up through and in contact with solids, and (5) force the gaseous agent to take such a route through the zone that high rates of gas flow may be used without having any undesirable effeet on the general direction the solids are moving. The functions of the bafile means set forth in (4) and (5) are increasingly important the finer the particle size of the solids.

Several structural means may be devised whereby the above requirements may be provided. Accordingly it is to be clearly understood that the present process is not to be restricted to the particular structural means shown and described for illustrative purposes for carrying out the process. Particularly convenient means and one relatively cheap is that internal arrangement which is shown in Figs. 2-6, 8 and 9. In this arrangement, there are shown the vertical heat exchange medium carrying tubes 22, and between those tubes there are shown various short pieces of light angle iron designated 29. These pieces of angle iron are so arranged that their length is placed horizontally and their angle is open downward. Placed in this manner between the heat exchanger tubes 22, each layer of angle irons 29 being disposed transversely to those on the layer below, each angle iron serves to receive the adsorbent descending from above and tube.

Ascending air is trapped beneath each piece of angle iron. To prevent its flow being concentrated at the ends of the angle irons against the walls of the chamber, each angle iron is pierced at several points along its heel forming a series of orifices 3|, these orificesbeing so located that those in one angle iron will be directly below the closed part of the next above I angle iron which crosses this part of the firstmentioned angle iron. In this manner each orifice distributes air into the space beneath the angle iron above it, yet air cannot pass directly upward through another orifice. In short, the

' arrangement is such that these orifices when assembled are not in register. It will be seen that by this arrangement the gas passes up through the chamber in a tortuous, substantially particlefree path but that the gas is in direct contact with the particles flowing along the bottom boundaries of the gas passages. The result of this arrangement is a very effective distribution and' redistribution of both downflowing adsorbent and upfiowing air,. coupled with an effective bringing ofthe adsorbent into-heat transfer re-.

lationship with the heat .transfer medium.fiowing within tubes 22-. Furthermore as stated hereinabove the use of-relatively high. air velocities are desired for practical regeneration. One

permit the use of rather-high air velocities withterial out of the apparatus. While baffles might be arranged so that gas would have to pass di-* of the prime features of battles 291s that they out boiling or blowing the clay or other marectly up through small portions of particles,

the sheltering of the path and redistribution of the particles should be frequent enough that the absolutely essential for successful operation and since careless operation might permigg-burning,

in these zones which are not provided .with fluid heat exchange medium, it may be found more practical at times to use this form of my apDa ratus, which omits the heat exchanger zonesn In Fig. 5, I also show channel members 33 which are placed transversely across the top row of angle irons, covering in row form the orifices 3! opening to the top of the chamber and thereby collecting therising air (see Figs. 8 and 9). Channel members 33 are provided with orifices 3| towhich are attached pipes 35 which lead upwardly to a point above the clay inlet opening of the throat I5 of hopper l4. This latter arrangement prevents the rising air from blowing the newly entering clay, which is above the angle irons, out of the chamber. Afurther feature of air pipes 35 is shown in Figs. 5 and 9, namely, a

of all of the air pipes 35 are bent outwardly in such fashion as to force the emerging air to flow" in a rotary manner thereby forming a centrifugal separator within the chamber, and, as a consequence of which the finely divided particles of dust carried by the air are separated out and drop back down while the particle-free air passes on up and out flue I8. It is to be understood, of

course, that if desired the air pipes 35 might lead-up to the flue or outlet and an external separator used as shown in Fig. 1.

In Fig. '7, I show in detail a preferred header structure which is particularly suitable for an apparatus such as shown in Fig. 5. As shown separate pipes 31, serve as manifolds to connect up rows of heat exchange tubes 22. Manifolds 31 are all in turn connected to a single master manifold pipe 38 through curved pipes 39. The

master manifold pipe 38 connects with pipe 24 (see Fig. 1) of the external heat transfer medium circuit. A similar header at the bottom of the chamber connects with pipe 23 of the external circuit.

As stated above, several structural means may be devised for effecting the desired baffling when I treating a flowing stream of small particles with a countercurrently flowing stream of gas. In Fig. 10 I show anotherbaiiie structure comprising winding fins which may be used in place'of the angle iron baiiies shown in the other cases. In fact, the fin baflies of Fig. 10 have certain advantages over the angle iron in that being welded to the tubes they give greater heat exchange surface to the tubes themselves, and,-

moreover, this fin structure has certain advantages from the construction standpoint,

In Fig. 10. tubes 22 are provided in a manner similar to that shown in the other cases which provide tubes, but instead of placing angle irons between the tubes, a metal fin 40 is welded to each tube, the fin being wound continuously along the tube as shown. It will be seen in Fig.

11 that the external peripheries of the fins 40 of adjaoenttubes are in vertical alignment. From I .what we have disclosed herein it will be apparcut that for best results these fins should be either so arranged or actually overlapping. In other words, there should not be any substantial cross area in the kiln above and below which, in

a straight vertical lineup through the length of the burner; '.thereis no baffling, since otherwise there would be short-circuitingf of the clay-in this area, and the clayin the center of this area might not be kept sufficiently close to heat change surfaces.. Of course, there might be a slight amount of this vertically free area before appreciably inferior results are encountered.

The object of having the fins wind along each tube is to provide winding substantially particlefree gas passageways up through the case underneath each fin which permit gas therein to directly contact the particles along at least one edge of the passageways. While the fins are shown as uniform helicalbaffles they may beof any equivalent structure which affords the desired result. i

In the preferred operation the particles fill the case, moving therethrough insubstantially a solid column of particles, and thereby form an outer-side wall to the gas passageways where the gas and catalyst are in direct contact. A further feature may be provided by using baffies of mesh wire construction, the mesh of which is too fine to permit passage of particles, and,

thereby, .the burning or reacting surface of the chamber is practically doubled since the burning or treating not only occurs along the above-mentioned "outer sidewall but also along the face of the baffles that the particles move over.

While the fins might be positioned at right angles to the tubes or even slanted slightly upward, most efilcient results are had by slanting th fins downwardly to give them a slope which is at least as great as the angle of repose of the particles being used. On the other hand the slope should not be too great, as the size of the gas passage is thereby reduced. We have found a slope of about 45 to be quite satisfactory for most uses. The pitch of the continuousspiral or helicalfln should not be so great that the particles more or less fall straight through the case, but rather should b at a more moderate pitch so that the particles substantially ride the baffles. Also if the pitch is too great no air passage is provided. It may be found of advantage to t have adjacent fins of opposite winding so that particles riding down thereon will be travelin in opposite directions, collide and thereby effect more thorough redistributing.

The size of the particles that may be treated in my process is limited by the air velocity required for feasible operation. For this reason clay particles treated should be of a granular nature for best results, for instance, 100 mesh or larger, as otherwise trouble may be encountered in obtaining a uniform downward flow of the solids. The invention is particularly feasible for regenerating filter clays of around 30-60 mesh, say particles of about 15 to about 100 mesh. However, it is to be understood the invention is not restricted as to the exact size of .the particles but rather to the general application of the process herein disclosed to solid particles of any size wherein the objects of the in vention are attained, particularly since particles of different materials, e. g., particles of ores to be roasted and spent porous particles to be regenerated, may vary appreciably in weight for the same size. Since the heat transfer in the present process should be principally by conductance, the treating zone, for best results, should stantial damage to the clay (or if other operations are being conducted, below temperatures which cause heat damage thereto) and, of course, at a temperature above which undue cooling occurs so that the regeneration (or other treatment) cannot proceed efiiciently. For instance, in the usual regeneration of filter clays and the like we preferably maintain the heat exchange medium at a temperature around 850-900 F. and never above about 1050" F. By so controlling the heat exchange medium and flowing a sufficient amount within sufficiently close indirect heat exchange with each particle, a close uniform temperature control is maintained over every particle so that no deleterious temperatures occur which cause injury to the particles .might be used in some instances, I greatly prefer be filled with the solid particles which then gravibe adjusted to a proper temperature for extracting or adding the necessary heat. Moreover, heat exchange medium must be "flowed in suflicient amount in close indirect heat exchange with every solid particle and then cooled or heated to readjust its temperature by means extraneous of the reaction heat before the medium's temperature reaches an undesired value. In this way the heat exchange medium in my invention continuously controls the temperature of the zone making immediate compensations for temperature changes whereby no deleterious temperatures occur. I

When the operation is first started the heat exchange medium may add some heat to help initiate the reaction or treatment, or at least the medium should not be at such a low temperature as to substantially hinder such initiation. After the operation is started the exchange medium is circulated throughout the zone adding or abstracting heat as required. In my invention the heat exchange medium is maintained at all points in the regenerating zone at a temperature below temperatures which cause subthe use of liquid heat exchange mediums since necessary pumping and pressure facilities for proper use of even the best gaseous mediums, e. g., hydrogen, would, in many instances, render the operation commercially impractical.

The liquid heat exchange medium to be used is preferably one which at the temperatures encountered is possessed of a low vapor pressure, a high specific heat, a suitable viscosity and is not corrosive to the usual metals and other materials which may be used in construction of the apparatus. Many normally solid materials in their fused state form excellent heat exchange mediums such as fused salts and fused metals and alloys. In the'regeneration of clay, I prefer the use the fused salts.- A particularly preferable mixture of this kind is a mixture of the alkali metal salts of nitric and nitrous acids. In certain cases suitable liquid heat exchange media might be found which have a boiling point around the desired operating temperature'in which case the heat exchange medium, although mostly in the liquid state, might undergo some transition whereby advantage could be taken of its heat of vaporization or condensation. By the use of liquid heat exchange media and by having them in sufficiently close proximity to all particles undergoing reaction an extremely close and uniform temperature control may be maintained.

In the preferred practice the heat exchange medium is maintained at substantially the temperature of the treatment being controlled, e. g., above the minimum temperature at which proper treating is obtained and below the minimum temperature at which undesirable heat injuries occur such as substantial damage to the particles or reaction. Such practice may be carried out effectively when the heat exchange medium is a liquid and has a relatively high specific heat and the structure of the apparatus is such that heat exchange medium is brought within close proximity to every granule in the apparatus.

Hence considerable fluctuations in temperature in either direction can be compensated by the liquid heat exchange medium without substantially altering its temperature and suitable coolmethod the liquid heat exchange medium would immediately and automatically ofiset the rise by absorbing any excess heat so that deleterious temperatures would not be created. Likewise, if the temperature fell off sharply so that normally the temperature would go so low that in- I efficient regeneration would result, this fluctuation likewise would be immediately andautomatically offset by the liquid heat exchange medium which would add heat to the cooling granules.

substantially the same temperature is maintained throughout, the apparatus operates without strain or difiiculty. x.

As a result of the close uniform temperature control afforded by my process, many important advantages are obtained.- For instance, the process of regenerating spent filter clays by burning is substantially revolutionized. Thus in my should not exceed about 1 /2 to 2 inches in order to afford proper temperat-ure'control, a distance of 1 inches being well suited to the regeneration of clay. Furthermore, it has been found that the volume expressed in cu. in., that may be occupied by the clay or other material, should be about A to 3 times the area of heat transfer surface, expressed in sq. in., (exclusive of the angle irons or other baflies). In the regeneration of fullers earth it is preferred tomaintain this ratio within the range of about 1/2 to 3/2.

With the above guides, the concept that the clay or other material is to be passed through a zone of substantial length to afford proper contact time with each particle in sufficiently close proximity to the heat exchange medium that no'deleterious temperature will be created at any point and the further concept that the burner is to be provided throughout with bafile means which proprocess, since I provide adequate temperature control, I preferably use not substantially more than the theoretical amount of air or oxygen to burn the carbon as contrasted to prior methods I which use large excesses of oxygen. As a. consequence the carbon on the clay or adsorbent usually furnishes all the necessary fuel for burning so that no additional fuel need be added, and, quite in contrast toiprior methods, my heat exchange medium may either extract or add heat to the clay. To offset overcooling and to heat the portion not under combustion in the prior processes, there have been various suggestions of heating indirectly with hot combustion gases. It is to be noted, howeverrthat these exchange mediums add heat rather than extract, and, moveover, being at high temperatures, above clay-damaging temperatures, they subject the clay to additional dangers.

In some treatments, as, for instance, in carbonizing some clays, the reaction or treatment may not give out sufilcient heat for its needs or it may even be endothermic. In such a case my heat exchange medium will supply heat to the operation rather than extract heat; nevertheless, the principles are the same with the medium being heated by the extraneous means rather than cooled and as before always maintainedbelow temperatures which cause heat damage to the .clay or other material or treatment being conducted.

As has been indicated hereinabove, one of the to specify the maximum distance that may be used for every operation to which my apparatus may be put. However, in general, this distance medi vide passages for the air, prevent channeling or short circuiting of the clay and air thereby permitting feasible air velocities to be used which do not stop the uniform counter fiow of the clay, it isbelieved any Worker in the .art will have'little trouble in designing the particular apparatus for his uses which incorporates the present invention and thereby permit him to carry out the present invention.

The rate of heat liberation per unit of time per unit of volume is a function of the mass velocity of adsorbent, of the amount of carbon to be burned therefrom, and of the mass velocity of the air. Experimentation has established that optimum conditions of burning occur in those ranges of mass velocities wherein the adsorbent is almost supported by the rising air, the upper limit being of course at air velocities so great that absorbent of the size being burned willnot fall but will-float. Since this velocity, will varywlth theapparent specific gravity of the clay, which apparentspecific gravity is a function of the real specific gravity and the particle size, the limiting velocity is not a single velocity, but a. rang ldefined as above. The inter-relation of adsorbent rate, carbon," and air rate maybe expressed best-as that combination of rates, which in the-case of fullers earth, for example, while not exceeding about 1150 F, under conditions of operation, will remove carbon at the rate of about 0.3 to about 2.0 pounds per hour per cubic foot of chamber volume for a broad range of possible operation, and

from about 0.5 to 1.5 pounds per hour per cubic foot of chamber volume for preferred operation.-

The mass velocity of heat transfer medium, of course, depends upon the specific heat and other characteristics of the medium. In operations where it is desirable to maintain the adsorbent at a relatively uniform temperature, the mass velocity is best defined as that mass velocity of heat exchange medium which will extract the required amount of heat while undergoing a temperature rise of not greater than about 50 F. and preferably of from 2 to 10 F.

That the process using a liquid .heat exchange is capable of close temperature control is shown by the graphs presented in'Figs. 12 and 13. Fig, 12 illustrates that the temperature can be maintained within very narrow limits even' when the nature of the clay feed isaltered drastically over short-time intervals. For the particu-' lar data of Fig..12 the oil content of the feed clay was varied from 0 to 5% at 30 minute intervals with clay turnover in the kiln once each hour.

The precise temperature control of which the process is capable is further illustrated in Fig. 13 which gives actual operating-temperature curves for various clay zones in my kiln for a period of several hours during a full-scale commercial operation. In this particular operation the clay rate was 21 -lbs./hr./cu. ft. of kiln volume and there was 7.2% of carbonaceous material on the unburned clay. The graph clearly shows that the temperatures in the various zones remained practically constant from P. M. to l. A. M. in an actual commercial operation.

Hereinabove it has been usually indicated that the temperature of burning should not rise above about 1150 F. This temperature is specific to materials of the nature of iullers earth, and for difierent materials having diflerent optimum re- Decolorlzatlion of Pa. chlorex refined Multiple MY hearth kiln Thus it will be seen the multiple hearth furgeneration temperatures, the proper specific teml5 nace has a diameter nearly 5 times greater and perature should be the basis 01' design and operaa weight times greater. Moreover, the above tion. data shows that per unit volume the contacting: To show specific application of the above broad surface of my kiln is about 50 times that of the': considerations of design, the following examples multiple hearth kiln which explains the tremenare given. Both are based upon regeneration of 20 dous capacity of my kiln with respect toits size." fullers earth, -60 mesh, from percolation flltra- Certain items of interest may be noted. "The tion of lubricating 011, using a molten salt heat maximum pressure dropfor air in designs have exchange medium, the clay having been washed, ing about 50% of the volume occupied by clay is steamed and removed from the filter in the usual about 3 inches of waterperfoot of chamber when manner, containing about 0.5% to 5.0% by weight as operating near atmospheric pressure. The of carbon" and up to. about 20% by weight of amount of air used is about 10% or more in excess moisture. The dimensional relations are asshown of that theoretically required. At burning tembelow: I perat'ures of about'1000-l050" F. the temperature control is easy and positive and no portion ofv KilnA m e 30 the clay need rise above 200 F, higherthan the temperature of..the heat transfer medium. Length of chamber lflfeet 13 feet. 7 The gain in filtration efllciency that may be 23532r tlit eiflflfiag its; iiiiiiii:::::::: iftfe. denved my d 8m siisrzszsznttss as a W1 pa. it?53155510313 otiiitfitiifitfil 31613552; 1'?" 7 i l i l e it fiwf .IIIII: {?."f$.". i x 5 lieved best shown by the tabular data set forth ggfffg gf gg f fl 3 in the following table, wherein clays burned on clay. I n a commerclal scale by my, present method are; g fggg ggggj gfi g ffifggf- :33 compared in percolation decolorizing efficiency clay). I 40 of various typical oils withuclays.burned-in one 57333; flf fgfigf of the best types of equipment at present avail Maximum clay thruput to burn 19. able, the clay. being used to exhaustion in per- ?Zfif 9" colation prior to each burn andibeing drained, Pressure drop olair for above rate- 30"water. 19" water. washed, and steamed as understood in the art, i g (Fresh burned clay was considered as efll The enormous'difl'erence in size .between an cient.) 1

Table Decolorization of Pa. chlorex refined on: residuum Decolon zation of Pa. short residuum on "81 duum.

Multi le Multi is v Multi 1e My process, decolorhearth iln, My process, decolorhearth 1l n, My process, decolorhearth iln,

lzation efllciency decolorization ization eflioiency decolorization [ration efliiciency decolorization efliciency efficiency I 1 efliciency Fresh burned 100% 100% l 88 56 (Discarded).

(Apparentl usable in- (Agaparcntly usable (Apparently usable indefinitely? eflnitely) definitely) Average etiiciency.. Approx. 100% orhigher 725% for 5 Approx. 100% for 18 75347 for 5 Agprox. 100% for 18 69 4% for 4 for 18 burns. urns. burns. burns. urns. urns.

No. 18 clays is approximately 100%.

asonsvo Decolorization of Mid- Dccolorization of coastal acid refined distillate E33 3 g gf f Multiple Multiple g gfgf hearth kiln, g gf fg fi hegrthlkiln, efliciency ggggz' efficiency gg Fresh burned 12 0 t1 fiziscard DD Y usable ined). definitely). Average cl- 100.1% 66.1%.

ficiencyfor 1O burns.

Thus it will be seen from the above table that a revolutionary improvement is obtained by the use of my method, 1. e., the efficiency of the clay regenerated by my method is substantially higher than clay which has been regenerated the same number of times in conventional kilns, in fact, clay regenerated by my commercial scale process has lost hardly any of its original efficiency even after 18 burns while the other clay is ready to be thrown away after 5 burns. Thus it will be noted the decolorizing efficiency of clay after 5 regenerations in the multiple hearth burner is reduced to around 50-55% of that offresh burned (new) clay, and, therefore, ready to be thrown away. The average efiiciency of these No. 1 to No. 5 clays is around 70% on the same basis. On the other hand, starting with fresh clay and conducting regenerations by my method, the eificiency of clay after even 18 regenerations is still around 95-100% and the average efiiciency of No. 1 to Since a value was not obtained for every burn, the exact average efficiency is not available; however, it can be seen that the average would be around 100% or even higher in some cases. The tremendously decreased "clay cost" which results by use of my process is obvious from the above. Thus it would appear that the clays may be efiiciently regenerated forever by my process. There is a purely mechanical loss of clay, however, from handling in apparatus now used which amounts to about 2% per burn so that after about 50 burns all of the original clay would be lost in this manner. It is to be further noted that the prior art operates at an average efficiency of around 70% while I operate at an average efficiency of around 100%. Therefore, in the filtering step alone, I obtain around 30% increased efficiency for the years operation. It will also be noted that in some instances the efliciency of my regenerated clay is above 100%. The probable reason for this is because the particular fresh burned clay was not initially prepared most efflciently and when carefully regenerated with proper control throughout, as provided by my process, the regenerated clay is more efficient than when freshly prepared.

In addition to the improvement advantage of positive temperature control whereby clay is reactivated to higher efliciency than that obtained by the prior art, as set forth above, the present method has several other distinct advantages over the commonly used methods. Not the least of these advantages is the fact higher throughput of clay per unit volume of burner is possible. I have varied the rate of clay throughput in my apparatus from 16 lbs./hr./cu. ft. of kiln volume to 75 lbs./hr./cu. ft. of kiln volume without any marked effect on the degree of reactivation. In certain cases the throughput is 15 to 30 times that of present multiple hearth burners. Quite ooviously a distinct improvement is afforded by this increased throughput rate in substantially reducing the time required to regenerate large batches of clay. The following data clearly demonstrates this advantage on clays of equal carbonaceous content,

Applicant's burner c l Eflectlve Eflective Clay feed rates, burning Clay rate, burning lbs./cu. ft./hr. surface, #[1 cu. ft./hr. surface,

sq. ttJou. it. sq. it./cu. it.

A further advantage of the present method is the fact it may be carried out in an apparatus which has no moving parts except the pump for circulating the! heat exchange medium. This not only makes construction and operation much simpler but considerably reduces the expense as compared, for example, to the commonly used multiple hearth burners wherein the rabble arms are rotated. v

Another important feature of the present invention is the efllcient utilization of the heat developed in burning. More heat is developed by burning most spent clays than is required and in my process the combustion is conducted so efliciently that no additional fuel need be added in the usual case, in fact, in the usual case of regenerating spent petroleum filter clays, heat i extracted by my process, being taken up by the liquid heat exchange medium and may be used for other purposes. Since the reaction is-exothermic this is only as it should be. However, in every other process now in use .heat must be added during the regeneration. For instance, the utilization of the heat developed by burning in the commonly used burners such as the multiple hearth type burner is so poor due to the amount of air used, loss to surroundings, etc., that additional fuel is added to burn off the impurities, the cost of thisadditional fuel for one average size refinery alone may be as high as $20,000 per year.

In the claims where I speak of solid particles or granules, I mean to include as a part of the particles or granules any solid or liquid matter that might be adhering to same as, for example,

the solid or liquid petroleum matter adhering to spent clay.

While the invention has been described in detail with respect to a preferred manner of burning clays, using a liquid heat exchange medium, it is to be understood, as set forth hereinabove, that the process is applicable to treating solid particles in general, and that other types of temperature control may be used, and that the invention includes the novel 'manner of contacting flowing solid particles with a gaseous agent whether temperature control is used or not. Accordingly, in the event an indirect heat exchange medium is not used the treating chamber need only contain the baffling means. Thus, in the type apparatus shown in Figs. 2-6, 8 and 9, the tubes 22 may be eliminated and additional angle irons inserted to cross the space occupied by the tubes. And, in the type apparatus shown in Figs. and 11, the tubes 22 could be replaced, for instance, with solid rods. Therefore, it is to be recognized that the present process affords a most efficient means for handling any solid particles in a continuous manner and contactin them'with a gaseous agent.

1 claim:

l. The method of regenerating spent adsorbent particles of clay-type contact material contaminated with carbonaceous impurities by burning oil? the impurities with air which comprises flowing the spent particles as a substantially compact column of particles under combustion conditions downwardly through a regenerating zone of suflicient length to afford proper regenerating time, flowing the air upwardly through the zone in direct contact with particles so as to burn off the carbonaceousmatter thereon, removing gases from the descending column of particles by withdrawing the gases, out of contact with the particles, from the interior of the column of particles to a point exterior to the column of particles, and closely maintaining the temperatureoffallfthe particles in the zone within a combustion temperature range within the minimum combustion temperature and the maximum combustion temperature that does not cause substantial heat damage to the particles.

2. A method of contacting solid particles of material with a gaseous agent which comprises flowing the particles as a substantially solid column of particles downwardly through a treating zone, flowing the gaseous agent countercurrently through the zone in direct contact with the particles, bafliing the flowing particles in such manner as to form a plurality of substantially continuous, particle-free paths for the gaseous agent through the downwardly flowing particles through which gas may flow upwardly the length of the zone in direct contact with the particles but without forcing its way through any substantial region of unbailled particles, flowing said gaseous agent through said paths, removing gaseous agent so flowed through said zone from contact with said particles by withdrawal thereof within said zone from contactwith said particles and passing withdrawn gas to a region exterior to and above saidcolumn, and subjecting the withdrawn gaseous agent in said region to centrifugal force to drop therefrom particles suspended therein.

3. A method of contacting solid particles of material with a gaseous agent which comprises flowing the particles as a substantially solid column of particles downwardly through a treating zone flowing the gaseous agent countercurrentlythrough the zone in direct contact with the particles, baffling the flowing particles insuch manner as to form a plurality of substantially continuous, particle-free paths for the gaseous agent through the downwardly flowing particles so that the gaseous agent passes upwardly through the zone in direct contact with the particles but without forcing its waythrough any substantial region of unbaiiled particles, withdrawing the gaseous agent from contact, with said particles within the interior of thecolumn of particles and passing the gaseous agent out of contact with the particles, to a point exterior to the column of particles.

4. A method of contacting solid particles of material with a gaseous agent within a given elevated treating temperature range which comprises flowing the particles as a substantial solid column of particles downwardly through a treating zone, flowing the gaseous agent through the zone in direct contact with the particles, bailiing the flowing particles in such manner as'to form a plurality of substantially continuous, particlefree paths for the gaseous agent through the downwardly flowing particles so that the gaseous agent passes through the zone in direct contact with the particles but without forcing its way through any substantial region of unbailled particles, withdrawing the gaseous agent from contact with said particles within the interior of the column of particles, passing the gaseous agent out of contact with the particles, to a point exterior to the column of particles, and flowing a suflicient amount of a gaseous heat exchange medium within sufficiently close indirect heat exchange to all the particles in said zone that the temperature of said particles is maintained closely within said temperature range.

5. A method of contacting solid particles of material with a gaseous agent which comprises flowing the particles as a substantially solid column of particles downwardly through a treating zone, flowing the gaseous agent through the zone in direct contact with the particles, baffling the flowing particles in such manner as to form a plurality of substantially continuous, particlefree paths for the gaseous agent through the downwardly flowing particles so that the gaseous agent passes through the zone in direct contact with the particles but without forcing its way through any substantial region of unbatlled particles, withdrawing the gaseous agent from contact with said particles within the interior of the column of particles and passing the gaseous agent out of contact with the particles, to a point exterior to the column of particles.

JOHN W. PAYNE. 

